JP5372308B2 - Fluid resistance reducing composition - Google Patents

Description

  The present invention relates to a fluid resistance reducing agent composition, a method for producing a fluid resistance reducing agent composition, and a method for reducing the fluid resistance of a hydrocarbon stream.

  When a fluid, such as a liquid hydrocarbon, is sent through a conduit, the friction resulting from the fluid stream causes a pressure drop that increases with distance from the feed point. Such frictional losses are also referred to as fluid resistance, which increases the energy and equipment costs required for fluid transport through the conduit.

Various polymeric materials have been used as additives in the fluid to reduce fluid resistance. Suitable materials were olefin polymers (homopolymers and copolymers), particularly very high molecular weight, amorphous, C ₃ -C ₃₀ α-olefin hydrocarbon soluble polymers. In order to facilitate the storage, transport and supply of fluid drag reducing polymeric materials, they have been provided in various forms.

  In addition to dry solid polymer, a slurry of ground polymer was used, but it tends to agglomerate over time. Polymer particles coated with an anti-agglomeration agent, on the other hand, have limited solubility in the hydrocarbon fluid to be fed. Polymer solutions and gels require special equipment for delivery and injection. They are also limited to a maximum concentration of 10% polymer by weight, which is not convenient.

International Patent Application Publication No. WO 97/01582 discloses that a non-solvent that polymerizes α-olefin in a solvent and precipitates the polymer as small particles is added to the resulting polymer solution. Disclosed are fluid drag reducing agent compositions made by separating the solvent and adding additional non-solvent and / or evaporating the solvent to further reduce the amount of solvent. The solvents used in this document are typically kerosene, jet fuel and paraffin and isoparaffin solvents. Typical non-solvents are C ₂ -C ₆ 1 monohydric alcohols and polyhydric alcohols, ethers, ketones and esters. Further, the aggregation inhibitor, for example, a metal salt of higher fatty acid can be added in an amount of 25 to 75% of the weight of the polymer.

International Patent Application Publication No. WO 98/16586 was made by coating poly-α-olefin particles with a non-aggregating agent that is, for example, fatty acid waxes (monoesters), fatty acid metal salts or fatty acid amides. Disclosed is a fluid resistance reducing agent composition. Then, the coated poly--α- olefin particles, <C ₁₄ 1 monohydric alcohols, are dispersed in <C ₁₄ glycols and polypropylene and polyethylene glycol ethers.

  The above technical solution in which the fluid drag reducing polymer is dispersed in alcohols, ethers, ketones and esters still has the disadvantage that the dispersion medium is not compatible with the hydrocarbon fluid whose fluid resistance is to be reduced.

Problems to be solved by the invention

  It is an object of the present invention to provide a fluid drag reducing agent composition that is effective and compatible with the hydrocarbon fluid to be fed through a conduit. The composition must also have a sufficiently high concentration and be easy to manufacture and handle. The ingredients of the composition must be inexpensive and readily available.

Means for solving the problem

[Means for Solving the Problems]
An object of the present invention is a method for producing a hydrocarbon fluid resistance reducing agent composition comprising a dispersion, the dispersion comprising:
(a) 1-60% of a polymer capable of reducing hydrocarbon fluid resistance, and
(b) 40-99% natural fat or natural oil, both based on the combined weight of (a) and (b)
Wherein the polymer is a hydrocarbon soluble alpha olefin polymer having Mw> 3 × 10 ⁶ g / mol and is in the form of a hydrocarbon gel. It was.
Preferably, the dispersion is also
(c) 0.1-50% additive, most preferably a dispersion stabilizer (based on the weight of (a), (b) and (c))
including.

Advantageously, components (a), (b) and (c) form at least 80%, most preferably at least about 90% of the total fluid resistance reducing agent composition. When all three components are present, the limits are 0.5-59.4% component (a), 20-98% component (b) and 0.1-50% component (c) ((a), (b) and (c) based on the combined weight).
A dispersion means a system in which dispersed phase particles are not bonded but separated from each other by a dispersion medium (Rompps Chemie-Lexicon, 7. Aufl. (1973), 2. Teil, 875).

As noted above, high molecular weight amorphous polymers that can reduce fluid resistance are well known per se and the skilled person knows how to choose them. Preferred polymers are high molecular weight (Mw> 3 × 10 ⁵ g / mol) C ₂ -C ₃₀ olefin polymers that are essentially non-crystalline, hydrocarbon soluble, and reduce hydrocarbon fluid resistance. It can be done. They can be homopolymers or copolymers of said olefins, whereby the comonomer is another olefin [see European Patent Application No. 0,223,889, page 3, lines 38-44 (herein incorporated by reference). Or, for example, divinyl monomers such as divinylbenzene or divinylsiloxane [see US Pat. No. 5,276,116, columns 2, 1.45, columns 3, 1.4 (incorporated herein by reference)]. Can be. Needless to say, a copolymer is a polymer containing more than one type of repeating unit, including terpolymers (Alger, MSM, Polymer Science Dictionary, 1990, Elsevier Appl. Sci., 86 page).

Preferably the polymer is an ultra high molecular weight (UHMW, Mw> 3 × 10 ⁶ g / mol) amorphous C ₃ -C ₃₀ α-olefin polymer, more preferably UHMW C ₄ -C ₂₀ α-olefin polymer, most UHMW C ₅ -C ₁₂ α-olefin polymers are preferred. Such polymers are used, for example, in International Patent Application Publication No. WO 97/01582 (incorporated herein by reference), which, on page 5, line 5-12, is 10 × 10 ⁶ g / mol. With a high molecular weight and a trade name that begins with FLO ™ and is sold by Baker Pipeline Products, a division of Baker Performance Chemicals, Inc. And poly α-olefins.

  Thus, the polyalphaolefin of the present invention is easily selected by those skilled in the art. They can also be readily manufactured, for example, by the method of Mack and Mack et al., Which is hereby incorporated by reference. See examples in US Pat. No. 4,415,714, columns 11-18, US Pat. No. 4,358,572, columns 7-10 and US Pat. No. 4,289,679, column 4. Here, the α-olefin is polymerized in the presence of a Ziegler-Natta system containing titanium chloride, an electron donor and an alkylaluminum cocatalyst, and the polymerization is stopped below about 20% conversion. Such polymers are soluble in hydrocarbon fluids and act as fluid drag reducers.

  Typical α-olefin homopolymers are polybutene-1, polyhexene-1, polyoctene-1, polydecene-1, polyhexadecene-1 and polyeicosene-1. Typical α-olefin copolymers are propene-dodecene-1 copolymer, butene-1-dodecene-1 copolymer, butene-1-decene-1 copolymer, hexene-1-dodecene-1 copolymer, octene-1-tetradecene-1 Copolymers, butene-1-decene-1-dodecene-1 copolymers, propene-hexene-1-dodecene-1 copolymers and the like. Preferred polymers are polyhexene-1, polyoctene-1, polydecene-1, polydodecene-1, polytetradecene-1, propene-dodecene-1 copolymer, butene-1-decene-1 copolymer, butene-1-dodecene-1 copolymer And hexene-1-dodecene-1 copolymer. Particularly preferred are polyhexene-1 and polyoctene-1.

In addition to the polymer that acts as a fluid drag reducer for hydrocarbon fluids, the claimed composition includes natural fats or natural oils. ^-1 preferably containing fatty oil. Fats or fatty oils that can be selected are plant, animal solid, semi-solid or liquid products, consisting essentially of a mixture of glycerin esters of higher fatty acids having an even number of carbon atoms. (Rompps Chemie-Lexicon, 7. Aufl. (1973), 2. Teil, 1101). Of course, single glycerin esters and synthetic glycerin ester mixtures can also be selected for the present invention. Corresponding synthetic fats or fatty oils are also within the scope of protection of the claims.

  Traditionally, natural fats and natural fatty oils are further divided according to the main individual fatty acids. Thus, fats that can be used in the present invention are lauric-myristic fatty fat-like coconut fat, palmitic fatty fat-like coconut fat and stearic fat-like cocoa butter. However, since fat melts only at a temperature of 24-47 ° C., it must be heated for dispersion, injection and distribution into the hydrocarbon fluid.

  Therefore, fatty oil is preferred over fat. Typical fatty oils are palmitic acid oils such as coconut oil, oleic acid-linoleic acid oils such as olive oil, linolenic acid oils such as linseed oil, shiso oil and hemp seed oil and erucic acid oils such as rapeseed oil and mustard oil. Preferred oils are based on or contain an essential amount of lauric acid, palmitic acid, stearic acid, oleic acid, linoleic acid and / or myristic acid. Such oils are soybean oil, sunflower oil, linseed oil, shiso oil, hemp seed oil, rapeseed oil and mustard oil, most preferably linseed oil and rapeseed oil. Other oils such as tall oil (based on fatty acids and resin acids such as abietic acid) can also be selected for the present invention. Fats and oils that can be selected for the present invention are described in Ulmanns Encyclopadie der Technischen Chemie, 3. Aufl., 7. Band, pp. 477-482 (by reference). See incorporated herein.

  The polymer can be simply mechanically dispersed in fat or oil, but the addition of a dispersion stabilizer is preferred. Preferred dispersion stabilizers are dispersants such as emulsifiers and other anti-agglomeration agents. For the purposes of the present invention, conventional emulsifiers can be readily selected that establish suitable boundary layer activity between the polymer and the fat or fatty oil. Such emulsifiers are provided by Ulmanns Encyclopadie der Technischen Chemie, 3. Aufl., 6. Band, pages 504-507 (incorporated herein by reference). Other useful anti-agglomeration agents can be selected from non-soap metal (eg, Zn) salts of fatty acids.

  However, preferred emulsifiers are 0 / W oil / water type anionic active species such as soaps and soap-like substances. Even more preferred are alkali metal, alkaline earth metal or ammonium soaps of fatty acids having 12 to 22 carbon atoms. Most preferred is an alkali metal or alkaline earth metal soap of a fatty acid on which the main component of fat or fatty oil is based. Such useful dispersion stabilizers are, for example, linseed oil or rapeseed oil sodium salt.

  The dispersion of the fluid resistance reducing composition of the present invention comprises 0.5 to 59.4% component (a) based on the combined weight of (a), (b) and (c) when a dispersion stabilizer is present. 20 to 98% of component (b) and 0.1 to 50% of component (c). See above.

  Preferably, the amount of the polymer (a) in the dispersion is 5-50% by weight, more preferably 10-40% by weight, based on the combined weight of (a), (b) and (c), Most preferably from about 20 to about 30% by weight.

  Independently, the amount of the natural fat or natural oil (b) in the dispersion is preferably from 50 to 95% by weight, based on the combined weight of (a), (b) and (c) Preferably it is 60 to 90% by weight, most preferably 70 to 80% by weight.

Further, independently, the amount of the dispersion stabilizer (c) in the dispersion is preferably 0.5 to 10% by weight, based on the combined weight of (a), (b) and (c). More preferably, it is 1 to 5% by weight, and most preferably 2 to 3% by weight.
The claimed composition can also include other ingredients that improve its properties.

  In addition to the fluid resistance reducing agent composition described above, the present invention also relates to a method for producing the fluid resistance reducing agent composition. According to the prior art, the production of useful fluid resistance reducing agent compositions has proved to be an almost easy task. As noted above, the polymer particles tend to agglomerate and have a low solubility or form a composition that is too dilute or not compatible.

  These problems are essentially due to the fact that the dispersion is (a) 1-60% of the previously described polymer capable of reducing fluid resistance and (b) 40-99% of the previously described. This was solved here by a method characterized in that it was formed from the fats or fatty oils described above (both percentages calculated on the combined weight of (a) and (b)).

  The dispersion can be formed solely by mechanical means, but the dispersion comprises (a) the amount of the polymer, (b) the amount of the fat or fatty oil and (c) the 0.1 to 0.1 described above. It is preferred if it is formed from 50% of the previously described additives, preferably a dispersion stabilizer (calculated on the combined weight of (a), (b) and (c)).

  Polymer (a), fat or fatty oil (b) and dispersion stabilizer (c) are essentially the corresponding components (a), (b) and (c) for the claimed fluid resistance reducing agent composition. ) Is selected as described above with respect to description.

  Advantageously, the polymer is provided in the form of a hydrocarbon gel. For example, the gel can comprise 1 to 20% by weight, preferably about 2 to about 10% by weight of the polymer, with the balance being essentially hydrocarbons and residual monomers if present. Typically, gels are formed when polymerizing α-olefin hydrocarbons to conversions below 20%.

  Before or during the contact of the polymer gel with the natural fat or natural oil, it is preferably disintegrated by feeding it through a disintegrating device, preferably a flaker or the like, and the size of the flakes or pellets is preferably 0.1 to 6.0 mm, most preferably 0.5 to 3.0 mm. A convenient flaker is a gear pump whereby the gear cuts a piece that then emerges in the form of the flake or pellet. Preferably the gel is fed to the suction side of the circulating gear pump of the device for dispersion of the components so that the disintegration of the gel occurs at the same time it is dispersed in the fat or oil (and dispersion stabilizer) .

  The claimed method can be carried out with or without pre-contacting the disintegrated gel with fat or fatty oil.

  According to one embodiment of the invention, the polymer is pre-contacted with and separated from the natural fat or natural oil at least once before it is finally dispersed in the natural fat or natural oil. Is done. Preferably, the precontacted fat or oil is the same fat or oil from which the polymer is finally dispersed. Precontacting is advantageously performed at room temperature, and the precontact weight ratio of the polymer gel to the fat or oil is preferably 1: 0.5 to 1:10, most preferably 1: 2 to 1: 4.

  After pre-contact, the polymer is concentrated. Concentration is preferably performed by separating the polymer from the fat or oil by gravimietrically or using a sieve, filter, cyclone, etc., by centrifugation, most preferably by vacuum filtration, after which the polymer is Dispersed in fat or oil. The amount is such that the above-described composition is achieved. Dispersion is preferably done by a dispersion mixer comprising a feed gear pump for feeding the polymer and a circulation gear pump and a return pipe for recirculating the polymer / fat or fatty oil mixture. Typical temperatures are 40-150 ° C, preferably 50-100 ° C. Typical dispersion times are 2 to 100 hours, preferably 10 to 50 hours.

  After the polymer is pre-contacted with and dispersed in the fat or fatty oil, unwanted fat or fatty oil is removed, preferably by sieving, most preferably by sieving using a 40-100 μm sieve. be able to. Next, the dispersion stabilizer is added. Preferably, under agitation, more preferably under vigorous agitation, most preferably by a homogenizer, such as one that includes a geared pump with a check valve and recirculation. Finally, the formed mixture can be stirred for 0.5 to 10 hours, preferably about 2 to about 6 hours, for example using a blade mixer at 50 to 200 rpm.

  According to another embodiment of the invention, the polymer is not pre-contacted, but directly with the fat or fatty oil and the dispersion stabilizer mixture. The polymer is then typically dispersed in the fat or oil by mixing at an elevated temperature, preferably 40-150 ° C, more preferably 50-100 ° C, so that most preferably the polymer is It takes the form of a gel. As at the end of the pre-contact embodiment, final agitation can be performed. See above.

  The dispersion stabilizer is preferably a soap, more preferably by reacting the fat or fatty oil with an alkali metal or alkaline earth metal base, most preferably a fatty or fatty oil used as a dispersion medium. Is produced in situ by partially saponifying it, thus forming a mixture of fat or fatty oil and dispersion stabilizer.

In addition to the claimed fluid resistance reducing agent composition and its manufacture, the present invention also relates to a method for reducing the fluid resistance of a hydrocarbon stream. This method is:
A. Providing a fluid resistance reducing agent composition according to the description of the product or manufactured according to the description of the method,
B. Characterized by a process comprising supplying a fluid drag reducing agent composition to a conduit in which hydrocarbons are flowing or flowing

  Preferably, the fluid resistance reducing agent composition is provided in an amount of about 1 to 200 ppm, preferably 10 to 100 ppm, and most preferably 20 to 80 ppm.

  The following examples, unless otherwise indicated, parts and percentages are based on weight, but are provided only to illustrate the present invention.

Measurement Method The method used to characterize the fluid drag reducing agent composition (hereinafter referred to as DRA) is roughly divided into physical properties (dry matter amount, viscosity) and actual performance characteristics (DPT, DFT, Visco50). be able to.

  The dry matter amount of the gel sample is determined by removing the gel solvent by evaporating in a heating chamber. Besides the polymer, the gel contains very little other solids, so the dry matter gives the polymer content of the product. Gel dry matter is a significant physical property as long as the performance achieved at the site of use depends on the amount of polymer dissolved in the fluid. That is, when supplying another product of equal weight or volume to the fluid, the most effective agent is supplied with the product having a large amount of dry matter.

  Viscosity is the dynamic viscosity (cP) measured by a Brookfield viscometer using different shear rates (eg 0.5, 1, 2.5, 5, 10, 20, 50 and 100 rpm).

  DPT (= Δ pressure vs. time) is a lifetime analysis. The sample to be tested is fed into a solvent circulation system maintained by a gear pump. By measuring the outlet pressure, the dissolution of the sample can be followed, and then the gradual disappearance of the fluid drag reducing effect as the sample passes through the pump one after the other. In DPT measurements, special attention is paid to the percent DPT, which is obtained as an integral by summing the difference between the reference pressure and the instantaneous pressure being measured. Fluid resistance reduction can be calculated using the following equation:

[Equation 1]
% Fluid resistance reduction rate = (p ₀ −p _s ) / p ₀ × 100
Where p ₀ is the measured drop that occurs when a test fluid without a fluid drag reducer is pumped through the test line, and p _s is the test fluid containing the fluid drag reducer. The measured pressure drop that occurs when pumped through the test line.

DFT (Δ force vs. time) is used to measure the efficiency of DRA in a vigorously stirred hydrocarbon solvent. In the measurement, the recorded percentage of decrease in fluid resistance represents the efficiency of DRA, and the better, the greater the% fluid resistance decrease rate. C ₀ indicates the amount of DRA (expressed in ppm) required to reach 67% of maximum efficiency under the conditions of measurement.

The Visco 50 test is based on measuring the dynamic viscosity of the sample. A 50 ppm solution of DRA is prepared and its viscosity is compared to the viscosity of the pure solvent. The results of the Visco 50 test contain information about the solubility of DRA and its ability to alter the viscoelastic properties of hydrocarbon fluids. The higher the Visco 50 value, the better the DRA.
Manufacturing

1. Equipment
-The dispersing device consisted of a conical bottom vessel equipped with a heating jacket and a circulating stirrer. The vessel cover had a water-cooled column with connections for effluent removal. It also had a separate cooler for liquefaction of the effluent gas.
-Another circulating gear pump and return pipe were connected to the bottom of the disperser.
-Another feed gear pump was provided to inject the polymer gel into the fatty oil (and dispersion stabilizer).
-A vacuum pump was provided, for example for filtration during and after the contact phase.
-A stator-rotor type homogenizer with stepless speed rotation control was also used.

2. Pre-contact method A gel containing 5-10% (see each example) polymer was given. The gel was then added to the fatty oil (rapeseed oil was used in the examples) and the weight ratio between the polymer gel and the fatty oil was 1: 2 to 1: 4 (see each example). . The contact temperature was 20 ° C. After pre-contact, the pre-contacted gel / fatty oil mixture was transferred to a vacuum sieve where the polymer gel particles were separated from the fatty oil.

  After pre-contact and separation, the final amount of fresh fatty oil was added to the separated polymer gel particles in a dispersion apparatus. The amount of gel corresponded to a polymer (dry matter amount) to fat or fatty oil weight ratio of 1: 3 to 1: 9 (see each example). The gel / fatty oil mixture was then mixed at 70 ° C. for 18 hours.

  After mixing, the excess fatty oil is removed by filtration using an 88 μm filter and the final amount of polymer and fatty oil (20-30% polymer and 70-80% fatty oil, according to examples) Gave. After removal, a final amount (2-3%, according to examples) of dispersion stabilizer was added and the final mixture was homogenized by a laboratory homogenizer (gear pump / check valve / recirculation). . After homogenization, the dispersion was still stirred for 4 hours using a laboratory stirrer.

3. Direct contact method, including the preparation of a dispersion stabilizer As a dispersion stabilizer, an appropriate amount of linseed fatty oil and its sodium salt (molar ratio eg 20:80) are mixed together at room temperature. Alternatively, linseed oil and 50% NaOH solution are mixed together at about 80 ° C. to form a linseed oil / sodium salt (soap) mixture having the same molar ratio. At elevated temperatures, possible volatile impurities are removed by evaporation. The mixture is kept in the described dispersion apparatus.

  The temperature is then adjusted to about 60 ° C. and the feed gear pump is started. The polymer gel is fed through a feed gear pump and sent through a small nozzle to a circulating stream of the mixture of linseed oil and its sodium salt. After feeding on the suction side of the circulating gear pump of the device, the polymer gel is cut into small pellets of 0.5-3.0 mm, which are easily dispersed in the hot mixture. The gel pellet is heated quickly, whereby the hydrocarbon gel solvent is removed by evaporation. Gel feeding is continued until the desired composition (see, eg, claims) is achieved.

  After dispersion, the product is finally homogenized by a laboratory hod-momizer as described above.

Examples Example 1 (Preliminary contact method)
The preparation of the dispersion was started by feeding a polymer gel based on 4.5 kg α-olefin, whose polymer content was 6.5% by weight in 11 kg rapeseed oil at room temperature. The resulting gel / oil mixture was vacuum sieved and the treated gel particles were collected for further processing. 1.8 kg of pure rapeseed oil was added to the polymer gel particles, and the resulting mixture was mixed at 70 ° C. for 18 hours. After mixing, excess rapeseed oil was removed with an 88 μm sieve, 30 g of rapeseed oil sodium salt was added as a dispersion stabilizer, and the mixture was homogenized using a laboratory hojimizer. Finally, the dispersion was mixed for 4 hours in a blade stirrer.
Product analysis

The weight of the polymer / oil mixture after vacuum filtration was 1.401 kg. The weight of the polymer / oil mixture after mixing at 70 ° C. was 1.192 kg. The polymer content of the final dispersion was 24.4%. DPT value was 31.7%, DR value was 29.0%, C ₀ value is 5.7, Visko 50 value was 0.234.

Example 2 (Preliminary contact method)
The preparation of the dispersion was started by feeding a polymer gel based on 1.8 kg α-olefin, whose polymer content was 6.5% by weight in 5.5 kg rapeseed oil at room temperature (20 ° C.). The resulting gel / oil mixture was vacuum sieved and the treated gel particles were collected for further processing. 0.9 kg of pure rapeseed oil was added to the polymer gel particles, and the resulting mixture was mixed at 70 ° C. for 18 hours. At the same time, hydrocarbons present in the gel were removed by evaporation and recovered for reuse. After mixing, excess rapeseed oil was removed with a 88 μm sieve, 20 g of rapeseed oil sodium salt was added as a dispersion stabilizer, and the mixture was homogenized for 5 minutes using a laboratory hojimizer. Finally, the dispersion was mixed for 4 hours in a blade stirrer.
Product analysis

The weight of the polymer / oil mixture after vacuum sieving was 1.031 kg. The weight of the polymer / oil mixture after mixing at 70 ° C. was 0.5 kg. The polymer content of the final dispersion was 25.8%. DPT value was 31.4%, DR value was 28.7%, C ₀ value is 7.8, Visko 50 value was 0.152.

Example 3 (direct contact method)
1850 g of linseed oil and 10 g of 50% NaOH solution were fed by vacuum into the vessel of the dispersion apparatus. The temperature was raised to 80 ° C. with stirring. The added compound was reacted for 1 hour while maintaining the temperature and the degree of vacuum.

The temperature was then adjusted to 60 ° C. and the gear circulation pump was started. A circulation pump circulated the mixture from the container back through the return pipe to the container. The 2 mm feed gear pump was then started and 18,700 g of fluid drag-reducing polymer gel was slowly fed through the 2 mm nozzle to the suction side of the circulation pump. The circulation pump cut the supplied polymer gel into 0.5-3 mm long pieces, which were dispersed in a hot mixture of oil and stabilizer.
After evaporation of the hydrocarbon solvent stopped, the dispersion was finally homogenized.

Analysis The dry matter amount of the homogeneous dispersion was about 24%. The fluid resistance reduction property was tested with a DPT device, and the viscosity was measured from a 50 ppm solution. DPT value was 34.5%, DR value was 25.5%, C ₀ value is 7.2, Visko 50 value was 0.159.

Example 4
In producing the dispersion, a fluid drag reducing polymer gel Necadd 547 ™ was used. In the polymerization of the polymer, using hexane cell N'nomi as monomers, solvent was not used.

  100 liters of soybean oil was fed with 30 liters of the Necadd 547 ™. The feeding of the gel is done by a flaking apparatus, where the gel is contacted with a 20 ° C. oil stream in the form of small flakes. The oil / gel mixture was transferred directly to a disperser equipped with a steam jacket, where the mixture was heated to 80 ° C. and hexene was removed by vacuum. It took 4 hours to remove the monomer.

  The mixture was then transferred to the tank. Remove excess oil from the mixture with vacuum sieve, add 200 g Stabilizer ES 2 and homogenize with laboratory homogenizer (gear pump / check valve / recirculation, homogenization time 5 min) went. The mixer was a 100 rpm paddle mixer.

  After vacuum sieving, the weight of the polymer / oil mixture was 3.2 kg. The polymer content of the final dispersion was 25%.

analysis
The DPT value was 32.3%, the DR value was 25.0%, the C ₀ value was 8.0, Visko 50 was 0.216, and the particle sizes were D 50 μm 312, D 90 μm 594 and D 10 μm 86.

Claims (25)

A method for producing a hydrocarbon fluid resistance reducing agent composition comprising a dispersion, the dispersion comprising:
(a) 1-60% of a polymer capable of reducing hydrocarbon fluid resistance, based on the combined weight of (a) and (b), and
(b) A hydrocarbon-soluble α formed from 40-99% natural fat or natural oil, based on the combined weight of (a) and (b), wherein the polymer has Mw> 3 × 10 ⁶ g / mol A process characterized in that it is an olefin polymer and is in the form of a hydrocarbon gel.
The method of claim 1, wherein the gel comprises 1-20% by weight of the polymer.
The method according to claim 1 or 2, wherein the gel has been disrupted by being fed through a disintegration device.
The gel The method of claim 3, wherein those that are collapsed into the natural fat or natural oil.
The dispersion is
(c) The dispersion stabilizer or other additive according to any one of claims 1 to 4, comprising from 0.1 to 50%, based on the combined weight of (a), (b) and (c). Method.
Wherein said natural fat or natural fatty oil is the main component of lauric acid, palmitic acid, stearic acid, oleic acid, claim 1-5 is a natural fat or fatty oil-based linoleic acid and / or myristic acid 1 The method described in the paragraph.
The process according to claim 6 , wherein the fatty oil is selected from soybean oil, sunflower oil, linseed oil, shiso oil, hemp seed oil, rapeseed oil and mustard oil.
The method according to any one of claims 5 to 7 , wherein the dispersion stabilizer is an emulsifier including a soap and an O / W type anionic emulsifier .
9. A process according to claim 8, wherein the dispersion stabilizer is an alkali metal, alkaline earth metal or ammonium soap of a fatty acid having 12 to 22 carbon atoms.
The method according to any one of claims 1 to 9 , wherein the amount of the polymer in the dispersion is 5 to 50% by weight.
The method according to any one of claims 1 to 10 , wherein the amount of the natural fat or natural oil in the dispersion is 50 to 95% by weight.
The method according to any one of claims 5 to 11 , wherein the amount of the dispersion stabilizer in the dispersion is 0.5 to 10% by weight.
13. A process according to any one of claims 1 to 12 , wherein the polymer is pre-contacted with and separated from the fat or oil at least once before it is dispersed in the natural fat or natural oil.
14. The method of claim 13, wherein the pre-contacted natural fat or natural oil is the same fat or oil in which the polymer is dispersed.
15. A process according to claim 13 or 14, wherein the polymer gel is pre-contacted with a natural fat or natural oil stream.
The process according to claim 15 , wherein in the pre-contact, the weight ratio between the polymer gel and the natural fat or natural oil is from 1: 0.5 to 1:10.
The process according to any one of claims 13 to 16 , wherein the polymer dispersion is concentrated after the preliminary contact.
18. A process according to any one of claims 13 to 17 , wherein after the precontacting and concentration, the polymer dispersion is redispersed in the natural fat or natural fatty oil.
The method according to any one of claims 5 to 18 , wherein the dispersion stabilizer is added after the polymer is dispersed in the natural fat or natural fatty oil.
20. The method of claim 19, wherein the dispersion stabilizer is added with stirring.
21. A process according to any one of claims 5 to 20 , wherein after the polymer and natural fat or natural oil are contacted and contacted with the dispersion stabilizer, the formed mixture is stirred for 0.5 to 10 hours.
13. A process according to any one of claims 5 to 12 , wherein the polymer is contacted with a mixture of the natural fat or natural oil and the dispersion stabilizer.
23. A method according to any one of claims 1 to 22 , wherein the polymer is dispersed in the natural fat or natural oil by mixing at an elevated temperature.
A dispersion stabilizer is produced in situ by reacting the natural fat or natural fatty oil with an alkali metal, alkaline earth metal or ammonium base, and the fat or fatty oil and dispersion stabilizer 24. The method according to any one of claims 5 to 23 , wherein a mixture is formed.
A. providing a fluid resistance reducing agent composition produced according to the method of any one of claims 1 to 24 ;
B. A method of reducing fluid resistance of a hydrocarbon stream by feeding the fluid resistance reducing agent composition to a conduit through which hydrocarbons are or will flow, wherein the fluid resistance reducing composition comprises: A process characterized in that it is fed in an amount of 1 to 200 ppm with respect to the amount of said hydrocarbon.